JP2012019730A - Lignocellulosic biomass saccharification pre-treatment device - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a lignocellulosic biomass saccharification pre-treatment device capable of effectively producing a pretreated material for saccharification in which ammonia gas is separated in a lignocellulosic biomass saccharification pre-treatment.SOLUTION: The lignocellulosic biomass saccharification pre-treatment device includes: a storage unit 3 which stores a substance mixture obtained by mixing lignocellulosic biomass and ammonia water and which obtains a pretreated material for saccharification dissociated or the like with lignin; a separation unit 4 which separates ammonia gas by heating a pretreated material for saccharification; a collection unit 5 which collects the ammonia gas as the ammonia water; a first heat recovery unit 25 which recovers heat-of-dissolution generated when ammonia gas is dissolved in water, and the heat supply units 8, 9, 10 which generate heat by using heat-of-dissolution recovered by the first heat recovery unit 25 and supply the heat to the separation unit 4.

Description

  The present invention relates to a lignocellulosic biomass saccharification pretreatment apparatus.

  Conventionally, ethanol is produced by obtaining a saccharified solution by saccharifying a substrate mixture obtained by mixing lignocellulosic biomass such as rice straw with a solvent using a saccharifying enzyme produced by a microorganism, and fermenting the saccharified solution. It has been known. Here, lignocellulosic biomass has a structure in which lignin is firmly bound to cellulose or hemicellulose.

  Therefore, by heating the substrate mixture in which lignocellulosic biomass and ammonia water are mixed, the lignin contained in the lignocellulosic biomass is dissociated, or the lignocellulosic biomass is swollen so that cellulose or hemicellulose can be saccharified. A pre-saccharification product is obtained.

  In order to reduce the amount of a pH adjuster that adjusts the pH of the saccharification pretreatment product to be saccharified to an optimum pH, it is known to perform saccharification pretreatment to obtain a saccharification pretreatment product from which ammonia has been separated. (For example, see Patent Document 1 and Patent Document 2).

Special table 2008-535524 gazette JP 2010-115162 A

  However, in the saccharification pretreatment described in Patent Document 1, 0.18 to 15% by mass of low-concentration aqueous ammonia is used, so that the saccharification pretreatment product is heated to separate ammonia from the saccharification pretreatment product. The heat energy increases and the manufacturing cost increases.

  Moreover, in the saccharification pretreatment described in Patent Document 2, a large amount of ammonia water is supplied to lignocellulosic biomass. Furthermore, ammonia is separated from the pre-saccharification product after the entire pre-saccharification product is heated to a predetermined temperature. Accordingly, there arises a disadvantage that the heat energy for separating ammonia from the pre-saccharification product increases and the production cost increases.

  The present invention eliminates such disadvantages, and when ammonia water is used for pre-saccharification of lignocellulosic biomass, the pre-saccharification pre-saccharification product from which ammonia has been separated can be efficiently produced. An object is to provide a processing apparatus.

  The lignocellulosic biomass saccharification pretreatment device of the present invention stores a substrate mixture obtained by mixing lignocellulosic biomass and ammonia water as a substrate, and the substrate mixture obtained by the mixing unit, A storage means for obtaining a pre-saccharification product that dissociates lignin from the substrate or swells the substrate, and a saccharification pre-process product supplied from the storage means is heated to continuously supply ammonia gas from the pre-saccharification product. A pretreatment device for lignocellulosic biomass saccharification comprising a separation means for separating the ammonia gas, the ammonia recovery means for dissolving the ammonia gas separated by the separation means in water and recovering it as ammonia water, and the ammonia recovery means A first heat recovery means for recovering heat of dissolution generated when ammonia gas is dissolved in water, and recovery by the first heat recovery means The a solution antipyretic generates heat supplied to the separating means as a heat source, the heat characterized by comprising a heat supply means for supplying to said separating means.

  In the lignocellulosic biomass saccharification pretreatment device of the present invention, first, the lignocellulosic biomass as a substrate and aqueous ammonia are mixed in a mixing means to form a substrate mixture.

  Next, the substrate mixture is stored by the storage means, and becomes a saccharification pretreatment product in which lignin is dissociated from lignocellulosic biomass or lignocellulosic biomass is swollen.

  In the present application, dissociation means that at least a part of the binding sites of lignin bonded to cellulose or hemicellulose of lignocellulosic biomass is broken. Swelling means that voids are generated in cellulose or hemicellulose constituting crystalline cellulose by the intrusion of liquid, or voids are generated inside cellulose fibers to expand.

  Next, after the pre-saccharification product is supplied from the storage unit to the separation unit, ammonia gas is continuously separated while being heated in the separation unit. As a result, a pre-saccharification product in which ammonia gas is separated from the pre-saccharification product can be obtained.

  On the other hand, the ammonia gas separated by the separation means is recovered as ammonia water by being dissolved in water by the ammonia recovery means, but the ammonia gas generates heat of dissolution when dissolved in water. For this reason, there is a concern that the temperature of the ammonia water rises, the solubility of ammonia decreases, and the recovery of ammonia gas becomes difficult.

  Therefore, in the lignocellulosic biomass saccharification pretreatment apparatus of the present invention, first heat recovery means is provided to recover heat of dissolution. The heat of dissolution is used as a heat source of a heat supply means to the separation means, and is supplied to a separation means for heating the pre-saccharification product to separate ammonia gas from the pre-saccharification product.

  Therefore, according to the lignocellulosic biomass saccharification pretreatment device of the present invention, the heat generated by the heat supply means is supplied to the separation means using the heat of dissolution as a heat source, thereby improving the energy efficiency and saccharification from which ammonia has been separated. A pretreatment product can be manufactured efficiently.

  Furthermore, according to the lignocellulosic biomass saccharification pretreatment device of the present invention, the ammonia gas separated from the saccharification pretreatment product by the separation means is dissolved in water to form ammonia water, and therefore, an auxiliary facility such as a safety valve is provided. There is no need to store in a pressure vessel.

  In the lignocellulosic biomass saccharification pretreatment apparatus of the present invention, the heat supply means includes a heat transfer means, a first heat pump means, and a second heat pump means, and the heat transfer means is the first heat transfer means. Heat of melting recovered by the heat recovery means is used as a heat source to heat the first heat medium circulating in the heat transfer means, to generate heat transferred to the first heat pump means, The heat pump means heats the second heat medium circulating in the first heat pump means by using the heat transferred by the heat transfer means as a heat source, and generates heat supplied to the second heat pump means. The second heat pump means uses the heat generated by the first heat pump means as a heat source, heats the third heat medium circulating in the second heat pump means, and is supplied to the separation means. heat Generation, it is preferable to.

  In the heat supply means, the temperature of the heat medium for cooling the ammonia water in the first heat recovery means is low, and the saccharification pretreatment product is heated in the separation means in order to sufficiently separate the ammonia gas from the saccharification pretreatment product. A high temperature of the heat medium is required.

  In the heat supply means using a single heat medium, the volume ratio of the heat medium circulating in the heat supply means increases and the circulation flow rate also increases. For this reason, an apparatus such as a compressor becomes large, equipment costs increase, and it becomes difficult to reduce manufacturing costs.

  Therefore, the heat supply means of the lignocellulosic biomass saccharification pretreatment apparatus of the present invention includes a first heat pump means using a second heat medium and a second heat pump means using a third heat medium. Furthermore, in order to efficiently distribute energy used for compression of the heat medium in the first heat pump means and the second heat pump means, a heat transfer means using the first heat medium is provided.

  The heat of dissolution recovered in the first heat recovery means is used as a heat source of the heat transfer means, and heats the first heat medium. Then, the heat generated by the heat transfer means is transferred to the first heat pump means.

  The heat transferred by the heat transfer means is used as a heat source for the first heat pump means, and heats the second heat medium. Then, the heat generated by the first heat pump means is supplied to the second heat pump means.

  Further, the heat generated by the first heat pump means is used as a heat source for the second heat pump means to heat the third heat medium. Then, the heat generated by the second heat pump means is supplied to the separation means.

  Therefore, according to the lignocellulosic biomass saccharification pretreatment apparatus of the present invention, heat of dissolution when ammonia gas is dissolved in water in the first heat recovery means can be recovered by the heat transfer means. Since the ammonia water is cooled by collecting the heat of dissolution, the ammonia gas can be easily recovered by preventing the temperature of the ammonia water from rising.

  Then, the generated heat is supplied to the separation means by the second heat pump means, and the pre-saccharification treatment product is heated, so that ammonia gas is sufficiently separated from the pre-saccharification treatment product and ammonia water is recovered in the ammonia recovery means. The amount can be increased.

  The lignocellulosic biomass saccharification pretreatment apparatus of the present invention comprises a second heat recovery means for recovering heat from the ammonia gas separated by the separation means, wherein the heat transfer means is the first heat recovery means. The first heat medium is heated by using the heat of dissolution recovered by the above and the heat recovered by the second heat recovery means as a heat source to generate heat transmitted to the first heat pump means. Is preferred.

  The lignocellulosic biomass saccharification pretreatment device of the present invention includes the second heat recovery means for recovering heat from the ammonia gas separated by the separation means, whereby the residual heat of the ammonia gas can be recovered. The energy efficiency of can be further increased. Further, according to the second heat recovery means, it is possible to easily dissolve the ammonia gas in water by recovering the residual heat from the ammonia gas.

  Further, in the lignocellulosic biomass pre-saccharification pretreatment apparatus of the present invention, the heat transfer means stores a first heat medium circulating in the heat transfer means and the first heat medium circulating in the heat transfer means. It is preferable to provide a flow rate adjusting means for adjusting a flow rate ratio between the heat medium and the second heat medium or the third heat medium.

  The lignocellulosic biomass saccharification pretreatment apparatus of the present invention includes a flow rate adjusting means, whereby a flow rate ratio between the first heat medium circulating in the heat supply means and the second heat medium or the third heat medium. To adjust the temperatures of the first, second, and third heat carriers. Therefore, fluctuations in the load of the first and second heat pump means can be suppressed with respect to fluctuations in the load of biomass and ammonia gas.

  Furthermore, in the lignocellulosic biomass pre-saccharification pretreatment apparatus of the present invention, it is preferable that the flow of the pre-saccharification product in the separation means and the flow of the third heat medium are counterflows.

  The saccharification pretreatment product supplied to the separation means releases ammonia by being heated in the separation means, so that the saccharification is performed after the saccharification pretreatment product is supplied to the separation means and discharged from the separation means. The concentration of ammonia water in the pretreated product decreases. Moreover, when the density | concentration of the ammonia water in a pre-saccharification processed material falls, the boiling point of ammonia water will rise.

  Therefore, the separation means is provided before the saccharification flowing in the separation means in order to sufficiently separate ammonia gas from the saccharification pretreatment product after the saccharification pretreatment product is supplied to the separation means and discharged from the separation means. It is necessary to set the temperature of the treated product to a boiling point corresponding to the ammonia water concentration.

  Accordingly, since the flow of the pre-saccharification product in the separation means and the flow of the third heat medium are counterflows, the period from when the pre-saccharification treatment product is supplied to the separation means until it is discharged from the separation means. The temperature difference between the pre-saccharification product and the third heat medium required for sufficiently separating ammonia gas from the pre-saccharification product can be realized, and efficient heat exchange can be performed.

The system block diagram of the lignocellulose biomass saccharification pre-processing apparatus of this invention.

  Next, embodiments of the present invention will be described in more detail with reference to the accompanying drawings.

  As shown in FIG. 1, the lignocellulosic biomass saccharification pretreatment device 1 of this embodiment is a substrate mixture obtained by mixing lignocellulosic biomass as a substrate (hereinafter sometimes abbreviated as biomass) and ammonia water. A mixer 2 to be obtained, a storage tank 3 for obtaining a pre-saccharification product obtained by dissociating lignin from biomass or swelling the biomass by storing the substrate mixture obtained by the mixer 2 at a predetermined temperature for a predetermined time, and before saccharification A separation device 4 that heats the processed product to separate ammonia gas from the pre-saccharification product, an absorption tower 5 that absorbs the ammonia gas separated by the separation device 4 into water and recovers it as ammonia water, and a separation device 4 And a transfer conduit 7 for deriving the pre-saccharification product from which ammonia gas has been separated and transferring it to the subsequent step 6.

  In addition, the heat transfer pipe through which the first heat medium flows in order to recover the heat of dissolution generated when the ammonia gas is dissolved in water by the absorption tower 5 and generate the heat that supplies the recovered heat of dissolution to the separation device 4 8, a first heat pump 9 using a second heat medium, and a second heat pump 10 using a third heat medium.

  An upper part of the mixer 2 is provided with an inlet 11 through which biomass is introduced, and an ammonia water supply conduit 12 for supplying ammonia water is connected. The ammonia water supply conduit 12 has an upstream end connected to an ammonia water tank 13 and is provided with a pump 14 on the way. Further, a storage tank 3 for storing the substrate mixture from the mixer 2 is connected to the lower part of the mixer 2.

  The storage tank 3 includes a powder feeder 15 at the bottom of the storage tank 3 that transfers the pre-saccharification product obtained by storing the substrate mixture for a predetermined time to the separation device 4.

  The separation device 4 is configured to heat the pre-saccharification product with heat supplied from the second heat pump 10 and continuously separate ammonia gas from the pre-saccharification product. For example, the separation device 4 causes the heat medium to flow through a multi-tube heating tube provided in the main body shell, rotates the multi-tube heating tube, and contacts the heating tube bundle with the pre-saccharification pre-treatment product. Is heated to dissipate ammonia from the pre-saccharification product to separate ammonia gas.

  The separation device 4 is connected to an upper portion thereof with an ammonia gas conduit 16 for extracting ammonia gas separated from the biomass in the pre-saccharification product. The ammonia gas conduit 16 is connected to the absorption tower 5 via a first heat exchanger 17 (corresponding to the second heat recovery means of the present invention).

  The ammonia gas conduit 16 includes a vacuum pump 18 that sucks ammonia gas and discharges it to the absorption tower 5 between the first heat exchanger 17 and the absorption tower 5. It is difficult to sufficiently dissipate ammonia by simply moving the pre-saccharification product from the separation device 4 to the discharge from the separation device 4 until it is heated and heated. Therefore, ammonia is sufficiently separated from the pre-saccharification product in the separation device 4 by sucking ammonia gas with the vacuum pump 18.

  When heat is recovered from the ammonia gas using the first heat exchanger 17, moisture in the ammonia gas is condensed. The first heat exchanger 17 is connected to a condensed water recovery conduit 19 in order to recover the condensed water. The condensed water recovery conduit 19 is connected to the absorption tower 5, and the recovered condensed water is used as water for generating ammonia water.

  Further, the separation device 4 has a transfer conduit 7 connected to the bottom. The transfer conduit 7 is connected to the post-process 6.

  The absorption tower 5 is configured to absorb the ammonia gas separated by the separation device 4 into water to form ammonia water, and store the ammonia water at the bottom. The absorption tower 5 is connected to an ammonia water outlet conduit 21 for extracting ammonia water at the bottom. The ammonia water outlet conduit 21 is connected to the ammonia water tank 13 via a pump 22.

  The absorption tower 5 is provided with a showering device 23 at the top of the absorption tower 5, and is connected to an ammonia water circulation conduit 24 that extracts ammonia water from the bottom of the absorption tower 5 and supplies the ammonia water to the showering device 23.

  The ammonia water circulation conduit 24 includes a second heat exchanger (corresponding to the first heat recovery means of the present invention) 25, and ammonia is introduced from the bottom of the absorption tower 5 between the absorption tower 5 and the second heat exchanger 25. A pump 26 is provided which sucks water and supplies it to the showering device 23 of the absorption tower 5.

  The ammonia water tank 13 includes an ammonia concentration sensor 27 that detects the concentration of the stored ammonia water, and a concentrated ammonia water supply conduit 28 that supplies concentrated ammonia water to the ammonia water tank 13.

  The heat transfer pipe 8 is a pipe through which, for example, a first heat medium such as water circulates in the pipe 8, and in the middle of the pipe 8, the first heat exchanger 17, the second heat exchanger 25, the second heat exchanger 3 A heat exchanger 29 and a buffer tank 30 are provided.

  The heat transfer pipe 8 sends the first heat medium stored in the buffer tank 30 to the first heat exchanger 17 and then to the third heat exchanger 29, and the first heat medium is transferred to the heat transfer pipe 8. It is provided with a pump 31 for circulation. In addition, the heat transfer pipe 8 includes a control valve 32 that adjusts the circulation flow rate of the first heat medium that circulates in the heat transfer pipe 8.

  The heat transfer line 8 connects the primary side of the first heat exchanger 17 for recovering heat from the ammonia gas, the primary side of the second heat exchanger 25 for recovering condensation heat, and the first heat pump 9. It is connected to the secondary side of the third heat exchanger 29 for supplying heat.

The first heat pump 9 includes a first circulation conduit 33 through which a second heat medium such as R134a (CF ₃ CH ₂ F) circulates, and a fourth heat exchanger 34 and an expansion valve are provided in the middle of the first circulation conduit 33. 35, a third heat exchanger 29, and a compressor 36.

  The first circulation conduit 33 includes a primary side of the third heat exchanger 29 for recovering heat from the first heat medium and a secondary side of the fourth heat exchanger 34 for supplying heat to the second heat pump 10. And connected to.

The second heat pump 10 includes a second circulation conduit 37 through which a third heat medium such as R245fa (CF ₃ CH ₂ CHF ₂ ) circulates. The separation device 4, the expansion valve 38, A third heat exchanger 34 and a compressor 39 are provided.

  The second circulation conduit 37 includes a primary side of the fourth heat exchanger 34 for recovering heat from the first heat pump 9 and a secondary of the separation device 4 for heating the saccharification pretreatment product to separate ammonia gas. Connected to the side.

  Next, the operation of the lignocellulosic biomass saccharification pretreatment device 1 of this embodiment will be described with reference to FIG.

  In the lignocellulosic biomass saccharification pretreatment device 1 of the present embodiment, first, lignocellulosic biomass is charged into the mixer 2 from the charging port 11. The lignocellulosic biomass is, for example, rice straw, and is supplied to the input port 11 after being pulverized by a cutter mill (not shown) so as to pass through a mesh having an opening of 3 mm.

  Next, the ammonia water in the ammonia water tank 13 is supplied into the mixer 2 by the pump 14 via the ammonia water supply conduit 12. At this time, the concentration of the ammonia water supplied into the mixer 2 is, for example, 25% by mass.

  The biomass and the ammonia water are supplied to the mixer 2 so that the dry mass of the biomass and the 25 mass% ammonia water are in a mass ratio of 1: 1.

  Next, the biomass and the ammonia water are mixed by the mixer 2 to form a substrate mixture in which the biomass and the ammonia water are mixed. The substrate mixture formed in the mixer 2 is stored in a storage tank 3 provided below the mixer 2 at a predetermined temperature, for example, 25 ° C., for a predetermined time, for example, 100 hours. While being stored in the storage tank 3, the biomass is swollen with aqueous ammonia, and a saccharification pretreatment product is formed in which the lignin bound to the cellulose and hemicellulose in the biomass is dissociated from the biomass.

  Next, the pre-saccharification product is supplied to the separation device 4 via the powder feeder 15. At this time, the pre-saccharification product supplied to the separation device 4 is heated by the third heat medium heated by the second heat pump 10. Then, ammonia is diffused from the pre-saccharification product in the separation device 4, and ammonia gas is separated from the pre-saccharification product.

  The separation means 4 of the present embodiment is configured such that the flow of the pre-saccharification product in the separation device 4 and the flow of the third heat medium are counterflows.

  The saccharification pretreatment product supplied into the separation device 4 moves in the separation device 4 from being supplied to the separation device 4 until being discharged from the separation device 4, and is heated in the separation device 4. Since ammonia is diffused, the concentration of ammonia water in the pre-saccharification product gradually decreases. For this reason, when the concentration of ammonia water in the pre-saccharification product decreases, the boiling point of the ammonia water increases.

  Therefore, the flow of the pre-saccharification product in the separation device 4 and the flow of the third heat medium are counterflowed, and the saccharification pre-treatment product is supplied to the separation device 4 and discharged from the separation device 4. Meanwhile, efficient heat exchange is performed by securing a temperature difference between the pre-saccharification product and the third heat medium necessary for sufficiently separating ammonia gas from the pre-saccharification product.

  The ammonia gas is sucked by a vacuum pump 18 provided in the ammonia gas conduit 16 and supplied to the absorption tower 5 via the first heat exchanger 17 of the ammonia gas conduit 16. The ammonia gas supplied to the absorption tower 5 is absorbed by the ammonia water showered from the showering device 23 and stored at the bottom of the absorption tower 5 as ammonia water.

  At this time, since excess heat is recovered by the first heat exchanger 17, the ammonia gas is easily absorbed by the ammonia water showered from the showering device 23. However, since the heat of dissolution is generated when the ammonia gas is dissolved in water, there is a concern that if the temperature of the ammonia water is increased by the heat of dissolution, the ammonia will not be sufficiently dissolved in the water.

  Therefore, in the present embodiment, when the ammonia water stored at the bottom of the absorption tower 5 is returned to the absorption tower 5 through the ammonia water circulation conduit 24, the second heat exchanger provided in the ammonia water circulation conduit 24 is provided. 25 to recover the heat of dissolution. As a result, in the absorption tower 5, a sufficient amount of ammonia gas is absorbed by the ammonia water showered from the showering device 23 and recovered as ammonia water.

  In the ammonia water tank 13, the ammonia concentration in the ammonia water stored by the ammonia concentration sensor 27 is detected, and concentrated ammonia water is supplied via the concentrated ammonia water supply conduit 28 in accordance with the detected ammonia concentration. The As a result, the ammonia water in the ammonia water tank 13 is adjusted to, for example, an ammonia concentration of 25% by mass and supplied to the mixer 2 via the ammonia water supply conduit 12.

  On the other hand, the pre-saccharification product from which the ammonia gas has been separated by the separation device 4 is transferred to the post-process 6 via the transfer conduit 7. The post-process 6 is a process in which cellulose contained in biomass is subjected to an enzymatic saccharification treatment, for example, by adding a predetermined amount of water and a saccharifying enzyme to a pre-saccharification product from which ammonia gas has been separated.

  At this time, the ammonia in the pre-saccharification product from which the ammonia gas has been separated becomes ammonia gas by being heated by the separation device 4, and the ammonia gas is sucked by the vacuum pump 18. Therefore, ammonia gas is sufficiently separated from the pre-saccharification product, and the pre-saccharification product in which a very small amount of ammonia, for example, about 10 ppm of ammonia remains, is transferred to the post-process 6.

  Here, the heat recovered by the first heat exchanger 17 and the second heat exchanger 25 is transmitted to the first heat pump 9 via the first heat medium circulating in the heat transfer pipe 8.

  For example, when water is used as the heat medium as the first heat medium used in the heat transfer pipe 8, the water stored in the buffer tank 30 is supplied to the primary side of the first heat exchanger 17 by the pump 31. As a result, the temperature of the water supplied to the first heat exchanger 17 rises by recovering the residual heat of the ammonia gas in the first heat exchanger 17.

  Then, the water that has recovered the residual heat of the ammonia gas in the first heat exchanger 17 is sent to the secondary side of the third heat exchanger 29. As a result, the water sent to the third heat exchanger 29 is cooled by supplying heat to the second heat medium of the first heat pump 9.

  The water cooled in the third heat exchanger 29 is supplied to the primary side of the second heat exchanger 25. As a result, the temperature of the water supplied to the primary side of the second heat exchanger 25 rises by recovering the heat of dissolution of the ammonia gas in the second heat exchanger 25. The water that has recovered the heat of dissolution of the ammonia gas in the second heat exchanger 25 is supplied to the buffer tank 30.

For example, when R134a (CF ₃ CH ₂ F) is used as the second heat medium, the first heat pump 9 first expands the R134a circulating through the first circulation conduit 33 by the expansion valve 35, and then performs the third heat exchange. Supply to the primary side of the vessel 29. As a result, R134a absorbs the heat transferred through the first heat medium in the heat transfer pipe 8 in the third heat exchanger 29 and rises in temperature.

  Next, R134a that has passed through the third heat exchanger 29 is supplied to the compressor 36 and compressed. R134a compressed in the compressor 36 is supplied to the secondary side of the fourth heat exchanger 34, and heats the third heat medium on the primary side of the fourth heat exchanger 34. Then, R134a that has passed through the fourth heat exchanger 34 is supplied to the expansion valve 35.

When the second heat pump 10 uses, for example, R245fa (CF ₃ CH ₂ CHF ₂ ) as the third heat medium, the R245fa circulating through the second circulation conduit 37 is first expanded by the expansion valve 38 and then the fourth heat Supply to the primary side of the exchanger 34. As a result, R245fa absorbs the heat generated by the first heat pump 9 in the fourth heat exchanger 34 and rises in temperature.

  Next, R245fa that has passed through the fourth heat exchanger 34 is supplied to the compressor 39 and compressed. R245fa compressed in the compressor 39 is supplied to the secondary side of the separation device 4 and heats the saccharification pretreatment product on the primary side of the separation device 4 to separate ammonia by diffusing ammonia from the saccharification pretreatment product. Then, R245fa that has passed through the separation device 4 is supplied to the expansion valve 38.

  On the other hand, the pre-saccharification product supplied to the separation device 4 is heated and ammonia is separated from the pre-saccharification product, and then transferred to the post-process 6.

  In the present embodiment, the flow rate of water that is the first heat medium circulating in the heat transfer pipe 8 is adjusted by the control valve 32 provided in the heat transfer pipe 8.

  By adjusting the flow rate of the water that is the first heat medium, the flow rate ratio with R134a that is the second heat medium of the first heat pump 9 or R245fa that is the heat medium of the second heat pump 10 is adjusted. Then, by adjusting the flow rate ratio between water as the first heat medium and R134a of the first heat pump 9 or R245fa of the second heat pump 10, the water as the first heat medium and the second heat medium of the first heat pump 9 The temperature of a certain R134a and the R245fa that is the third heat medium of the second heat pump 10 is adjusted, and the amount of heat generated by the second heat pump 10 and supplied to the separation device 4 is adjusted.

  As a result, the load fluctuations of the first heat pump 9 and the second heat pump 10 are suppressed with respect to load fluctuations such as biomass and ammonia gas.

DESCRIPTION OF SYMBOLS 1 ... Lignocellulosic biomass saccharification pre-processing apparatus, 2 ... Mixer, 3 ... Storage tank, 4 ... Separation apparatus, 5 ... Absorption tower, 6 ... Post process, 7 ... Transfer conduit, 8 ... Heat transfer pipe, 9 ... First DESCRIPTION OF SYMBOLS 1 heat pump, 10 ... 2nd heat pump, 17 ... 1st heat exchanger, 25 ... 2nd heat exchanger, 29 ... 3rd heat exchanger, 30 ... Buffer tank, 33 ... 1st circulation conduit, 34 ... 4th heat Exchanger 37 ... second circulation conduit.

Claims (5)

A mixing means for obtaining a substrate mixture obtained by mixing lignocellulosic biomass as a substrate and aqueous ammonia;
Storing the substrate mixture obtained by the mixing means, dissociating lignin from the substrate, or obtaining a pre-saccharification product in which the substrate is swollen;
A lignocellulosic biomass saccharification pretreatment device comprising a separation means for heating the saccharification pretreatment product supplied from the storage means and continuously separating ammonia gas from the saccharification pretreatment product,
Ammonia recovery means for dissolving ammonia gas separated by the separation means in water and recovering it as ammonia water;
First heat recovery means for recovering heat of dissolution generated when ammonia gas is dissolved in water by the ammonia recovery means;
And a heat supply means for generating heat to be supplied to the separation means using the heat of dissolution recovered by the first heat recovery means as a heat source, and supplying the heat to the separation means. Cellulosic biomass saccharification pretreatment equipment. In the lignocellulosic biomass saccharification pretreatment device according to claim 1,
The heat supply means comprises a heat transfer means, a first heat pump means, and a second heat pump means,
The heat transfer means heats the first heat medium circulating in the heat transfer means using the heat of dissolution recovered by the first heat recovery means as a heat source, and is transmitted to the first heat pump means. Generate heat,
The first heat pump means heats the second heat medium circulating in the first heat pump means by using the heat transferred by the heat transfer means as a heat source, and is supplied to the second heat pump means. Generate heat,
The second heat pump means heats the third heat medium circulating in the second heat pump means by using the heat generated by the first heat pump means as a heat source, and supplies the heat to the separation means A lignocellulosic biomass saccharification pretreatment device characterized in that In the lignocellulosic biomass saccharification pretreatment device according to claim 2,
A second heat recovery means for recovering heat from the ammonia gas separated by the separation means;
The heat transfer means heats the first heat medium using the heat of dissolution recovered by the first heat recovery means and the heat recovered by the second heat recovery means as a heat source, and A lignocellulosic biomass saccharification pretreatment apparatus, which generates heat transmitted to one heat pump means. In the lignocellulosic biomass saccharification pretreatment device according to claim 2 or 3,
The heat transfer means stores a first heat medium circulating in the heat transfer means, and the first heat medium and the second heat medium or the third heat circulating in the heat transfer means. A lignocellulosic biomass saccharification pretreatment device comprising flow rate adjusting means for adjusting a flow rate ratio with a medium. In the lignocellulosic biomass saccharification pretreatment device according to any one of claims 2 to 4,
The lignocellulosic biomass saccharification pretreatment apparatus, wherein the flow of the pre-saccharification product in the separation means and the flow of the third heat medium are counterflows.

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